Process for removing metal species in the presence of hydrogen and a porous material and polyester polymer containing reduced amounts of metal species

ABSTRACT

A process for removing metal species from a composition comprising contacting: a. an oligomer mixture stream comprising the monomers of a partially aromatic polyester polymer and at least one metal species, or b. a molten polyester polymer stream comprising partially aromatic polyester polymers and at least one metal species, with a non-catalytic porous material in the presence of hydrogen to produce a treated stream containing a reduced amount of at least one metal species. There is also provided a composition comprising a partially aromatic polyester polymer having an It.V. of at least 0.50 produced in a direct esterification melt phase process, from greater than 0 to less than 50 ppm antimony, and less than 40 ppm cobalt. There is also provided a composition comprising partially aromatic polyester polymers having an It.V. of at least 0.50 produced in an ester exchange melt phase process, from greater than zero to less than 5 ppm titanium, and less than 10 ppm manganese.

FIELD OF THE INVENTION

This invention pertains to polyester polymer and processes for themanufacture thereof, and in particular to processes for the productionof polyester polymers having a reduced amount of metal species bycontacting oligomer mixtures and/or polyester polymers in a melt phasewith a non-catalytic porous material in the presence of hydrogen, and topolyester polymers having reduced amounts of metal species.

BACKGROUND OF THE INVENTION

Metal species such as metallic ions or elemental metallic residues cancause problems in many industrial chemical processes. For example, metalions or elemental metallic residues present in a reaction feed maydeactivate a catalyst; and metal ions in electronic cleaning solventsmay lead the electronic devices to malfunction. In the manufacture ofpolyester polymers, the presence of metal particles added as catalystscan cause packaging made from these polymers to appear hazy, yellow incolor, and often continue to be catalytically active therebycontributing to the formation of acetaldehyde and other color bodies.

Ion-exchange resins are widely used to remove metal ions. Since theseresins are made of organic polymers, and are usually used at ambienttemperature or slightly above the ambient temperature. Zeolites andactivated carbon are widely used as adsorbent for purification orseparation. Activated carbon can be used to purify water by absorbingalkaline earth metal ions; zeolite A can remove moisture by acting adesiccant. However, little is known on how to remove metal ions orelemental metallic residues from a system that is highly viscous or fromsolid solutions at ambient temperature or at slightly highertemperature.

We have discovered that it is desirable to remove metal species in themelt phase reaction for the production of polyester polymers. Thecontinual catalytic effects of some metals have been dealt with by theaddition of various catalyst deactivators or thermal stabilizers. Somestabilizers, especially those of the phosphorous acid or esters ofvarious phosphorous compounds are added in quantities which reduce ametal such as antimony to its elemental state, which can contribute tothe darkening of the polymer if large amounts of the antimony have to bereduced. It would also be desirable to recover some of these metals asthey may no longer significantly contribute to further advantagesdownstream once their function as polymerization and/or esterificationcatalysts has concluded.

BRIEF DESCRIPTION OF THE INVENTION

There is now provided a process for removing metal species from acomposition comprising contacting:

-   -   a. an oligomer mixture stream comprising the monomers of a        partially aromatic polyester polymer and at least one metal        species, or    -   b. a molten polyester polymer stream comprising partially        aromatic polyester polymers and at least one metal species,        with a non-catalytic porous material in the presence of hydrogen        to produce a treated stream containing a reduced amount of at        least one metal species.

There is also provided a composition comprising a partially aromaticpolyester polymer having an It.V. of at least 0.50 produced in a directesterification melt phase process, from greater than 0 to less than 50ppm antimony, and less than 40 ppm cobalt.

There is also provided a composition comprising partially aromaticpolyester polymers having an It.V. of at least 0.50 produced in an esterexchange melt phase process, from greater than zero to less than 5 ppmtitanium, and less than 10 ppm manganese.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 a is a process flow diagram illustrating a dedicated stand alonevessel containing porous particles receiving a feed of oligomer mixture.

FIG. 1 b illustrates that esterification products may be split into twostreams; one oligomer stream is taken as a side draw and introduced forhydrotreating and the other stream introduced directly into apolycondensation zone.

FIG. 2 is a schematic process flow diagram illustrating hydrotreating amolten polyester polymer stream, in which zone V23 and the zone V24 maybe operated in separate units (FIG. 2 a) or in an integrated unit withthe high polymerizer vessel split into different zones within the samevessel (FIG. 2 b).

FIG. 3 illustrates a process flow diagram in which the molten polyesterstream from a polycondensation zone is used as the feed to a fixedparticle bed.

FIG. 4 illustrates a process flow diagram in which amorphous solidpolyester polymers or crystallized polyester polymers or solid statepolymerized polyester polymers, either in the form of virgin particles,scrap, or post consumer recycle polymer, is melted, or diluted orde-polymerized, and fed to a vessel loaded with the porous particles toreduce the metal content of the polymer stream.

DETAILED DESCRIPTION OF THE INVENTION

The present invention may be understood more readily by reference to thefollowing detailed description of the invention. It is to be understoodthat this invention is not limited to the specific processes andconditions described, as specific processes and/or process conditionsfor processing plastic articles as such may, of course, vary.

It must also be noted that, as used in the specification and theappended claims, the singular forms “a”, “an” and “the” include pluralreferents. References to a composition containing “an” ingredient or “a”polymer is intended to include other ingredients or other polymers,respectively, in addition to the one named.

Ranges may be expressed herein as “within” or “between” or from onevalue to another. In each case, the end points are included in therange. Ranges expressed as being greater than or less than a valueexclude the end point(s).

By “comprising” or “containing” or “having” is meant that at least thenamed compound, element, particle, or method step etc must be present inthe composition or article or method, but does not exclude the presenceof other compounds, materials, particles, method steps, etc, even if theother such compounds, material, particles, method steps etc. have thesame function as what is named.

It is also to be understood that the mention of one or more method stepsdoes not preclude the presence of additional method steps or interveningmethod steps between those steps expressly identified.

The It.V. values described throughout this description are set forth indL/g units as calculated from the inherent viscosity measured at 25° C.in 60/40 wt/wt phenol/tetrachloroethane. The inherent viscosity iscalculated from the measured solution viscosity. The following equationsdescribe such solution viscosity measurements and subsequentcalculations to Ih.V. and from Ih.V. to It.V:η_(inh) =[ln(t _(s) /t _(o))]/Cwhere

-   -   η_(inh)=Inherent viscosity at 25° C. at a polymer concentration        of 0.50 g/100 mL of 60% phenol and 40% 1,1,2,2-tetrachloroethane    -   ln=Natural logarithm    -   t_(s)=Sample flow time through a capillary tube    -   t_(o)=Solvent-blank flow time through a capillary tube    -   C=Concentration of polymer in grams per 100 mL of solvent        (0.50%)

The intrinsic viscosity is the limiting value at infinite dilution ofthe specific viscosity of a polymer. It is defined by the followingequation:$\eta_{int} = {{\lim\limits_{C\rightarrow 0}\left( {\eta_{sp}/C} \right)} = {\lim\limits_{C\rightarrow 0}\quad{\ln\quad\left( {\eta_{r}/C} \right)}}}$where

-   -   η_(int)=Intrinsic viscosity    -   η_(r)=Relative viscosity=t_(s)/t_(o)    -   η_(sp)=Specific viscosity=η_(r)−1

Instrument calibration involves replicate testing of a standardreference material and then applying appropriate mathematical equationsto produce the “accepted” I.V. values.Calibration Factor=Accepted IV of Reference Material/Average ofReplicate DeterminationsCorrected IhV=Calculated IhV×Calibration Factor

The intrinsic viscosity (ItV or η_(int)) may be estimated using theBillmeyer equation as follows:η_(int)=0.5 [e ^(0.5×Corrected IhV)−1]+(0.75×Corrected IhV)

In one aspect of the invention, there is provided a process for removingmetal species from a composition comprising contacting:

-   -   a. an oligomer mixture stream comprising the monomers of a        partially aromatic polyester polymer and at least one metal        species, or    -   b. a molten polyester polymer stream comprising partially        aromatic polyester polymers and at least one metal species,        with a non-catalytic porous material in the presence of hydrogen        to produce a treated stream containing a reduced amount of at        least one metal species.

Either an oligomer mixture or a molten polyester polymer stream contactsa fixed bed or a slurry of non-catalytic porous material. The oligomermixture is produced by esterifying reactants in an esterification zonein the presence of metal species to form an oligomer mixture comprisingthe monomers used as the repeating unit residues in the partiallyaromatic polyester polymer made in the polycondensation zone, and atleast one metal species. Examples of monomers used as the repeating unitresidues in a polyester polymer include bis-hydroxyalkylterephthalatemonomers or bis-hydroxyalkylnaphthalate monomers. An example of a commonmonomer is bis-hydroxyethylterephthalate (BHET). The oligomer mixturemay contain condensed monomers forming oligomers having 2 to less than 7repeating units, such that the average number of repeat units may rangefrom 0.8 to less than 7.0. The esterification reaction can be a directesterification processor an ester exchange process. The metal species inthe oligomer mixture may be present due to the addition of catalysts inan ester exchange reaction, or due to the impurities in the terephthalicacid feed present as a result of the not completely removing catalystmetal species added to an oxidation reactor for making crudeterephthalic acid.

A molten polyester polymer stream comprises partially aromatic polyesterpolymers such as those which may be found in the polycondensation zoneof a melt phase process for the manufacture of partially aromaticpolyester polymers, or those which may be found in solid post melt phasepolyester polymers, such as amorphous or crystallized pellets, solidstate polymerized polymers, end use applications such as packaging(trays and bottles) and films and sheets, or post consumer recycledpolymer. The molten polyester polymer stream typically has an averagenumber of repeat units of 7 or more and generally up to about 20. In theprocess of the invention, solid post melt phase polyester polymers areremelted to produce a molten polyester stream. Regardless of the sourceof polyester polymers, the molten stream contains metal species. Suchmetal species in the polyester polymers are typically present due to theaddition of catalysts used to manufacture terephthalic acid or polyesterpolymers, or added as reheat agents to the polymer.

Thus, in a melt phase embodiment, reactants may be esterified (direct orester exchange) in a esterification zone in the presence of metalspecies to form an oligomer mixture and metal species, and subsequentlypolycondensing the oligomer mixture in a polycondensation zone to form amolten polyester polymer, optionally in the presence of additionalamounts of metal species and/or different types of added metal species,and thereafter solidifying the molten polyester polymer. At any pointafter the oligomer mixture is formed and before the molten polyesterpolymer is solidified, at least a portion of the oligomer mixture ormolten polyester polymer contacts the porous material in the presence ofhydrogen. All of the oligomer mixture stream or the polyester polymerstream present in the melt phase reaction may be brought into contactwith the suspension or fixed bed of non-catalytic porous material, oronly a portion of any one or both of these streams may be brought intocontact with the porous material. Thus, all or a portion of the productof the esterification zone, such as when at least 90% conversion of thereactants to the esterification reactor is obtained; or all or a portionof the stream flowing between the esterification zone and thepolycondensation zone; or all or a portion of the stream produced in aprepolymer reaction zone within the polycondensation zone; or all or aportion of the polyester polymer near or after completingpolycondensation and molecular weight build up from a finishing reactor;or the finished polyester polymer stream flowing to a machine forsolidifying the molten stream into fibers, strands, preforms, orparticles, may be brought into contact with the porous material beforethe stream is solidified.

Since the porous material is effective to remove metal species in thepresence of hydrogen, its location may also be dependent upon whether ornot one desired to remove the metal species from the stream. Forexample, in the event that a polycondensation catalyst metal is added tothe prepolymerization reactor in a polycondensation zone, the locationof contact between a stream and the porous particles is desirably beforethe point of polycondensation catalyst addition. Locating the porousmaterial prior to the polycondensation zone is applicable to a directesterification and an ester exchange process, and in the latter process,a further advantage can be had in that the quantity of ester exchangecatalyst metal which is usually deactivated before polycondensation cannow also be significantly reduced to further avoid the possibility ofexchange catalyst activity during polycondensation or to reduce theamount of deactivator added at the conclusion of esterification.Alternatively, if one desires to add a polycondensation catalyst to theesterification zone, the contact location between the stream and porousmaterial may occur between the first esterification reactor and thesecond or subsequent esterification reactors, followed by adding thepolycondensation catalyst to the second or subsequent esterificationreactors. The particular location of the porous material in a melt phasepolymerization reaction will be dependent largely upon the viscositylimitations of the feed stream and the location where metals are addedin the process which one does not desire to remove.

Typical metal species present in an oligomer mixture or polyesterpolymer composition include cobalt, antimony, titanium, manganese, zinc,calcium, zirconium, copper, iron, nickel, chromium, vanadium, ormixtures thereof. By a metal species is meant the metal present as acompound or alloy, and in any oxidation state, including elemental metaland metal in the +1, +2, +3, +4 oxidation states. In the broadest aspectof the invention, at least a portion of at least one metal species isremoved, and is preferably removed onto the non-catalytic porousmaterial. Desirably, the quantity of at least one of the metal speciespresent in an oligomer mixture of polyester polymer is reduced by atleast 50%, measured as the difference between the metal species underconsideration before contact with the porous material and after contactwith the porous material in ppm. Preferably, at least one of said metalspecies is reduced by at least 75%.

The process of the invention is particularly well adapted to removingmetal species from viscous materials. Thus, in one embodiment, themolten polyester polymer stream contacting the porous material has anIt.V. of at least 0.1 dL/g, or at least 0.3 dL/g, such as what may betypically experienced in a melt phase process. In a particularlypreferred process, there is provided a melt phase reaction in which theamorphous polyester polymer produced from such melt phase process has anIt.V. of at least 0.70 dL/g, or at least 0.72 dL/g, or at least 0.75dL/g. With the removal of at least a portion of metal species from theoligomer mixture or polymer melt, fewer metal atoms are available tocatalyze the formation of acetaldehyde or cause the formation of colorbodies, thereby allowing one to continue reacting the polymer mixture tohigher It.V.'s in the melt phase where the formation of acetaldehyde andcolor bodies is especially prevalent.

The porous material contacting the oligomer mixture or the moltenpolyester polymer is non-catalytic, meaning that the porous material isnot a hydrogenation catalyst that would hydrogenate aromatic rings toalicyclic rings under the contact conditions. It is undesirable toproduce a treated stream containing polymers with repeat units whichdiffer from the repeating units of the feed polyester stream, whichwould occur if the porous material was, for example, a member of theplatinum series of metals. One of the advantages of the invention isthat the porous materials can be used as a guard bed to remove metalspecies from the polyester stream which could possibly poison the streamby converting the repeating units to different species. While the porousmaterial should not be once which is catalytic in the sense ofhydrogenating the aromatic rings, the porous materials may, however,accelerate, stabilize, or decelerate the reaction rate or rate at whichthe molecular weight of the oligomer mixture or molten polyester polymerbuilds upon contact with the porous material under the reactionconditions. Thus, the non-catalytic porous material may affect thedegree of conversion, specificity, and rate, but does not hydrogenatethe aromatic rings to any substantial degree. While the porous materialis not designed to act as a catalyst, it is recognized thatcatalytically active impurities may be present on or in the porousmaterial as contaminants in small amounts which could hydrogenate thearomatic rings, and/or the reaction conditions may favor the conversionof aromatic rings to alicyclic rings due to the presence of hydrogenunder pressure and high temperature. Thus, up to about 100 ppm of thearomatic rings in the melt phase stream may be hydrogenated afterpassing the stream over the porous material, which is deemed to be aninsubstantial degree of conversion. The method for detecting thepresence of hydrogenated rings is by methanolysis; i.e., a sample of thetreated oligomer is first degraded by methanolysis and then both GC andLC are used to determine whether dimethyl cyclohexanecarboxylate(DMCD)—the product of the hydrogenated aromatic ring—is present. Otherequivalent methods may also be employed.

Typical hydrogenation catalysts are normally found in the platinumfamily, such as platinum, palladium, iridium, osmium, rhodium, and theirbinary or tertiary mixture. The porous materials used in the invention,however, are not in the platinum family and do not substantiallycatalyze the hydrogenation of the polyester polymer aromatic rings underthe reaction conditions used to remove the metal species.

Examples of non-catalytic porous materials include carbon, graphite,activated carbon, silicon carbide, alumina, silica and mixtures thereof.The pore volume of the porous materials is suitably 0.1 cc/g to 0.8cc/g, and suitable pore diameters range from 0.8 nm to 40 nm. Materialshaving a wide range of surface area are suitable, such as those having asurface area ranging from 0.5 to 2000 m²/g. It is desirable that thesurface area of the porous material ranges from 300 to 1100 m²/g inorder to increase the number of metal species atoms adsorbed. At a givensurface area, it is desirable to have larger pore diameter and a largepore volume. It is also more desirable to use a particle having a highersurface area. However, in the presence of hydrogen, we have found thatporous particles having a small pore diameter within the stated rangealong with a moderate pore volume and surface area will provide goodlevels of impurity absorption.

The porous particle size desirably ranges from 2 mm to 50 mm, preferablyfrom 3 mm to 20 mm. In a fixed bed mode, which is preferred, theparticle size is generally in the range of 3 to 30 mm. However, theprocess may also be practiced as a suspended slurry, in which case theparticles can be much smaller, in the range of 0.1 mm to 2 mm.

The oligomer mixture or molten polyester stream flows across the porousmaterial. The porous material is slurried or preferably in a fixed bedsuch that the particles do not flow downstream with the oligomer mixtureor polyester stream. The porous particle may be loaded into an existingesterification or polycondensation reactor. Alternatively andpreferably, a guard bed may be provided in an integrated melt phaseprocess, or a dedicated stand-alone vessel loaded with the particles isprovided into which the oligomer mixture or polyester polymer stream isfed and discharged as a reduced metal stream. The liquid hourly spacevelocity (LHSV) of the molten polyester stream over the fixed bed isdesirably a value ranging from 0.2 to 40 hour⁻¹, more preferably from 1to 15 hour⁻¹.

Hydrogen gas is brought into contact with the oligomer mixture or moltenpolyester polymer stream. Although the porous material is non-catalytic,without the presence of hydrogen, the metal species are not removed. Thegas hourly space velocity GHSV of hydrogen over the fixed bed isdesirably a value ranging from 5 to 1000 hour⁻¹, preferably from 100 to400 hour⁻¹. Without being bound to a theory, it is believed that themetal species are captured on the porous support because hydrogenreduced the metal cation to a lower oxidation state or to elementalmetal, thereby providing an atom having a larger atomic radius andenabling the support to capture the larger atom within its pores.Whatever the mechanism, however, we have found that the porous supportis effective in the presence of hydrogen to capture metal speciesimpurities in the feed stream.

The hydrogen gas fed to the porous particle bed or the gaseousatmosphere in contact with the stream and porous particle bed has ahigher volume % of hydrogen gas than does air. The hydrogen gas fed tothe porous particle bed, or the gas composition contacting the streamand porous particles, is preferably at a hydrogen concentration of atleast 10 vol. % hydrogen, or at least 20 vol % hydrogen, or at least 50vol % hydrogen, and more preferably at least 80 vol % hydrogen or atleast 90 vol % hydrogen and most preferably about 100 vol %. Suitablehydrogen partial pressure within the vessel or zone containing theporous material ranges from 1 to 10 kg/cm² when calculated at 250° C.and 150 psi gauge pressure.

The pressure on the molten polyester stream when contacting the porousmaterial in the presence of hydrogen is positive, and desirably rangesfrom 10 to 2000 psig, and more typically from 50 to 150 psig. Thetemperature of the oligomer mixture or the polyester stream in thepresence of hydrogen ranges from 150 to 300° C., and more typically from200 to 280° C.

The process of the invention is effective to remove at least a portionof at least one of the metal species present in the oligomer mixture ofmolten polymer stream to produce a reduced metal stream. In oneembodiment, at least one of the metal species present is reduced by atleast 50%, and preferably by at least 75%. In another embodiment of theinvention, the oligomer mixture or molten polyester stream containscobalt as the metal species in one or more oxidation states, and theamount of cobalt is reduced by at least 50% to less than 20 ppm. Inanother alternative embodiment, or in addition, after contact with theporous material, the reduced metal stream contains less than 5 ppmtitanium, less than 20 ppm zinc, less than 20 ppm manganese, less than20 ppm calcium, and less than 20 ppm magnesium. Other metal specieswhich may be present in the polyester polymer composition or in theoligomer mixture that can be effectively reduced in amount by theprocess of the invention include zirconium, chromium, iron, nickel, andcopper. The oligomer mixture and the molten polyester polymer streamcontacting the porous material contains less than 10 ppm germanium, andis preferably free of germanium metal species.

In yet another embodiment, the process of the invention is effective toreduce the amount of each metal present in the oligomer mixture or themolten polyester polymer in an amount of over 10 ppm by at least 25%, orat least 50%, and most preferably by at least 65%.

The process can be practice continuously, in a batch mode, or in asemi-batch mode. When the capacity of the porous material to adsorb themetal species drops to an undesirable level, the metal may be recoveredfrom the porous material. Techniques for recovering the metal speciesinclude metal refining, pyrometallurgy, hydrometallurgy, andelectrometallurgy, as described in Ullmann's Encyclopedia of IndustrialChemistry, 5^(th) Edition, Volume 16, pp 375-387, VCH, 1990.

There is also now provided unique compositions comprising partiallyaromatic polyester polymers which are amorphous or partiallycrystallized. There is provided, in one embodiment, a compositioncomprising partially aromatic polyester polymers having an It.V. of atleast 0.50 produced in a direct esterification melt phase process,antimony present in an amount of greater than 0 and less than 50 ppmantimony, preferably less than 30 ppm, and cobalt in an amount rangingfrom 0 to less than 40 ppm, preferably less than 25 ppm. In thisembodiment, antimony atoms are present, but are present in the statedamounts, while the amount of cobalt may be zero either because it wasnot added to the melt phase or it is totally removed.

The polymer composition may be solid or molten. In the case of a solid,the polyester polymers in the composition may be amorphous, which is thenatural state of the polymer product solidified from the melt phaseprocess or from an injection molding machine to make bottle preforms, orthe polymers may be partially crystallized. Partial crystallinity may beimparted to the polyester polymers in the composition by isolating theamorphous polymer as a solid, followed by applying conventionalcrystallization techniques. It is not always the case, however, that themelt phase product is isolated as an amorphous solid polymer. Forexample, the melt phase product may be fed directly to an underwatercutter and immediately crystallized underwater without exposing the cutpolymer to air. Alternatively, the underwater cut polymer may be rapidlydried and crystallized in air by the latent heat within the cutparticles before the particles have a chance to fall below the Tg of thepolymer. Thus, the stated amounts of metal species may also be presentin a crystalline polymer. The degree of crystallinity should be at least25%, or at least 30%, or at least 35%, or at least 40%.

The polymer composition may also be molten. A molten composition ispresent in a melt phase process in which the It.V. of the polymer equalsor exceed 0.50 dL/g, in a melt to preform process, or in a melt to chipprocess. In each case, the molten stream contains the stated amounts ofmetal species.

The polyester polymer may contain optional metals. Such metals and theiramounts are less than 5 ppm titanium, less than 20 ppm zinc, less than20 ppm manganese, less than 20 ppm calcium, less than 20 ppm magnesium,and/or less than 10 ppm germanium, more preferably less than 5 ppmgermanium. In this embodiment, one or more of the metals may optionallybe absent such that the amount is zero, but preferably, at least one ofthe aforesaid metals is present in an amount of greater than 0.

The polyester polymer product preferably also has an It.V.greater than0.70 dL/g, or greater than 0.72 dL/g. This It.V. is obtained withoutsolid state polymerization techniques typically used to advance themolecular weight of the polymers in the solid state. The It.V. isdesirably obtained from the melt phase process for the manufacture ofthe polyester polymers.

In another embodiment, there is provided a composition comprisingpartially aromatic polyester polymers having an It.V. of at least 0.50produced in an ester exchange melt phase process, titanium present in anamount of greater than 0 and less than 5 ppm titanium, and less than 10ppm manganese, preferably less than 7 ppm manganese. In this embodiment,titanium is present but in an amount of less than 5 ppm, preferably 3ppm or less, and the amount of manganese may be zero, either because iswas not ever added or because it was removed totally in the process. Asin the embodiment above, this polymer composition may be solid ormolten, amorphous or crystalline, and may have an It.V. of at least 0.70dL/g or at least 0.72 dL/g.

In each case, the partially aromatic polyester polymers arethermoplastic homopolymers, or thermoplastic copolymers obtained by theaddition of modifier compound to provide more than two types orrepeating units. A thermoplastic polymer is distinguishable from liquidcrystal polymers and thermosetting polymers in that thermoplasticpolymers have no ordered structure while in the liquid (melt) phase,they can be remelted and reshaped into a molded article, and liquidcrystal polymers and thermosetting polymers are unsuitable for theintended applications such as packaging or stretching in a mold to makea container.

The partially aromatic polyester polymer contains residues of aromaticrings and contains polyester linkages. Desirably, the partially aromaticpolyester polymer contains alkylene terephthalate or alkylenenaphthalate repeating units in the polymer chain. More preferred arepolyester polymers which comprise:

-   -   (a) a carboxylic acid component comprising at least 80 mole % of        the residues of terephthalic acid, derivates of terephthalic        acid, naphthalene-2,6-dicarboxylic acid, derivatives of        naphthalene-2,6-dicarboxylic acid, or mixtures thereof, and    -   (b) a hydroxyl component comprising at least 60 mole %, or at        least 80 mole %, of the residues of ethylene glycol or propane        diol,        based on 100 mole percent of carboxylic acid component residues        and 100 mole percent of hydroxyl component residues in the        polyester polymer.

Typically, polyesters such as polyethylene terephthalate are made byreacting a diol such as ethylene glycol with a dicarboxylic acid as thefree acid or its dimethyl ester to produce an ester monomer and/oroligomers, which are then polycondensed to produce the polyester. Morethan one compound containing carboxylic acid group(s) or derivative(s)thereof can be reacted during the process. All the compounds containingcarboxylic acid group(s) or derivative(s) thereof that are in theproduct comprise the “carboxylic acid component.” The mole % of all thecompounds containing carboxylic acid group(s) or derivative(s) thereofthat are in the product add up to 100. The “residues” of compound(s)containing carboxylic acid group(s) or derivative(s) thereof that are inthe product refers to the portion of said compound(s) which remains inthe oligomer and/or polymer chain after the condensation reaction with acompound(s) containing hydroxyl group(s).

More than one compound containing hydroxyl group(s) or derivativesthereof can become part of the polyester polymer product(s). All thecompounds containing hydroxyl group(s) or derivatives thereof thatbecome part of said product(s) comprise the hydroxyl component. The mole% of all the compounds containing hydroxyl group(s) or derivativesthereof that become part of said product(s) add up to 100. The residuesof hydroxyl functional compound(s) or derivatives thereof that becomepart of said product refers to the portion of said compound(s) whichremains in said product after said compound(s) is condensed with acompound(s) containing carboxylic acid group(s) or derivative(s) thereofand further polycondensed with polyester polymer chains of varyinglength.

The mole % of the hydroxyl residues and carboxylic acid residues in theproduct(s) can be determined by proton NMR.

In another embodiment, the polyester polymer comprises:

-   -   (a) a carboxylic acid component comprising at least 90 mole %,        or at least 92 mole %, or at least 96 mole % of the residues of        terephthalic acid, derivates of terephthalic acid,        naphthalene-2,6-dicarboxylic acid, derivatives of        naphthalene-2,6-dicarboxylic acid, or mixtures thereof, and    -   (b) a hydroxyl component comprising at least 90 mole %, or at        least 92 mole %, or at least 96 mole % of the residues of        ethylene glycol, based on 100 mole percent of the carboxylic        acid component residues and 100 mole percent of the hydroxyl        component residues in the polyester polymer.

The reaction of the carboxylic acid component with the hydroxylcomponent during the preparation of the polyester polymer is notrestricted to the stated mole percentages since one may utilize a largeexcess of the hydroxyl component if desired, e.g. on the order of up to200 mole % relative to the 100 mole % of carboxylic acid component used.The polyester polymer made by the reaction will, however, contain thestated amounts of aromatic dicarboxylic acid residues and ethyleneglycol residues.

Derivates of terephthalic acid and naphthalane dicarboxylic acid includeC₁-C₄ dialkylterephthalates and C₁-C₄ dialkylnaphthalates, such asdimethylterephthalate and dimethylnaphthalate.

In addition to a diacid component of terephthalic acid, derivates ofterephthalic acid, naphthalene-2,6-dicarboxylic acid, derivatives ofnaphthalene-2,6-dicarboxylic acid, or mixtures thereof, the carboxylicacid component(s) of the present polyester may include one or moreadditional modifier carboxylic acid compounds. Such additional modifiercarboxylic acid compounds include mono-carboxylic acid compounds,dicarboxylic acid compounds, and compounds with a higher number ofcarboxylic acid groups. Examples include aromatic dicarboxylic acidspreferably having 8 to 14 carbon atoms, aliphatic dicarboxylic acidspreferably having 4 to 12 carbon atoms, or cycloaliphatic dicarboxylicacids preferably having 8 to 12 carbon atoms. More specific examples ofmodifier dicarboxylic acids useful as an acid component(s) are phthalicacid, isophthalic acid, naphthalene-2,6-dicarboxylic acid,cyclohexanedicarboxylic acid, cyclohexanediacetic acid,diphenyl-4,4′-dicarboxylic acid, succinic acid, glutaric acid, adipicacid, azelaic acid, sebacic acid, and the like, with isophthalic acid,naphthalene-2,6-dicarboxylic acid, and cyclohexanedicarboxylic acidbeing most preferable. It should be understood that use of thecorresponding acid anhydrides, esters, and acid chlorides of these acidsis included in the term “carboxylic acid”. It is also possible fortricarboxyl compounds and compounds with a higher number of carboxylicacid groups to modify the polyester.

In addition to a hydroxyl component comprising ethylene glycol, thehydroxyl component of the present polyester may include additionalmodifier mono-ols, diols, or compounds with a higher number of hydroxylgroups. Examples of modifier hydroxyl compounds include cycloaliphaticdiols preferably having 6 to 20 carbon atoms and/or aliphatic diolspreferably having 3 to 20 carbon atoms. More specific examples of suchdiols include diethylene glycol; triethylene glycol;1,4-cyclohexanedimethanol; propane-1,3-diol; butane-1,4-diol;pentane-1,5-diol; hexane-1,6-diol; 3-methylpentanediol-(2,4);2-methylpentanediol-(1,4); 2,2,4-trimethylpentane-diol-(1,3);2,5-ethylhexanediol-(1,3); 2,2-diethyl propane-diol-(1,3);hexanediol-(1,3); 1,4-di-(hydroxyethoxy)-benzene;2,2-bis-(4-hydroxycyclohexyl)-propane;2,4-dihydroxy-1,1,3,3-tetramethylcyclobutane;2,2-bis-(3-hydroxyethoxyphenyl)-propane; and2,2-bis-(4-hydroxypropoxyphenyl)-propane.

As modifiers, the polyester polymers may contain comonomers such asisophthalic acid, naphthalane dicarboxylic acid, cyclohexanedimethanol,and diethylene glycol.

The polyester pellet compositions may include blends of polyalkyleneterephthalates and/or polyalkylene naphthalates along with otherthermoplastic polymers such as polycarbonate (PC) and polyamides. It ispreferred that the polyester composition should comprise a majority ofthe polyester polymers, more preferably in an amount of at least 80 wt.%, or at least 95 wt. %, and most preferably 100 wt. %, based on theweight of all thermoplastic polymers (excluding fillers, inorganiccompounds or particles, fibers, impact modifiers, or other polymerswhich may form a discontinuous phase). It is also preferred that thepolyester polymers do not contain any fillers, fibers, or impactmodifiers or other polymers which form a discontinuous phase.

Compositions of the invention in the form of solid particles may be fedto an extruder suitable to make containers or sheet. The particles maybe:

-   -   A) dried in a drying zone to produce dried particles;    -   B) introduced into a melting zone;    -   C) melted in a melt processing zone, and    -   D) formed into an article such as a preform or tray.

Once the particles have been dried, they are introduced into a meltprocessing zone to form molten polyester polymer, followed by forming anarticle such as a sheet or a molded part. Any conventional techniqueused to melt particles and form articles therefrom can be used. Suitablemelt processing zones include extruders equipped with a barrel, one ormore screws in the barrel, a motor to turn the screw, heating elementsto direct heat through the barrel to the particles, and a die platethrough which the molten polymer is forced. The die may be a sheet die,optionally connected to a thermoforming mold. Another melt processingzone is an injection molding machine equipped with the same features,except that a nozzle is used instead of a die through which the polymeris forced into a runner system that directs the polymer into one or moremold cavities. An example of a molded part includes a bottle preform(parison).

In the melt processing zone to produce an article, or in the melt-phaseprocess for making the polyester polymer, other components can be addedto the composition of the present invention to enhance the performanceproperties of the polyester polymer. These components may be added neatto the bulk polyester, may added as a dispersion in a liquid carrier ormay be added to the bulk polyester as a polyester concentrate containingat least about 0.5 wt. % of the component in the polyester let down intothe bulk polyester.

The types of suitable additives which can be added to the meltprocessing zone or to the melt phase reaction or to solid compositionsas a particle/particle blend include crystallization aids, impactmodifiers, surface lubricants, stabilizers, denesting agents,antioxidants, ultraviolet light absorbing agents, metal deactivators,colorants, nucleating agents, acetaldehyde lowering compounds, reheatrate enhancing aids, sticky bottle additives such as talc, and fillersand the like can be included. The resin may also contain small amountsof branching agents such as trifunctional or tetrafunctional comonomerssuch as trimellitic anhydride, trimethylol propane, pyromelliticdianhydride, pentaerythritol, and other polyester forming polyacids orpolyols generally known in the art. All of these additives and manyothers and their use are well known in the art and do not requireextensive discussion. Any of these compounds can be used in the presentcomposition.

In each of these embodiments, the articles of manufacture are notlimited, and include sheet and bottle preforms. The bottle preforms canbe stretch blow molded into bottles by conventional processes. Thus,there is also provided in an embodiment the bottles made from thespheroids of the invention, or made by any of the processes of theinvention, or made by any conventional melt processing technique.

Not only may containers be made from compositions made according to theprocess of this invention, but other items such as sheet, film, bottles,trays, other packaging, rods, tubes, lids, filaments and fibers, andother molded articles may also be manufactured using the polyestercompositions of the invention. Made from polyethylene terephthalatepolymers, beverage bottles suitable for holding water or carbonatedbeverages, and heat set beverage bottles suitable for holding beverageswhich are hot filled into the bottle are examples of the types ofbottles which are made from the crystallized spheroids of the invention.

The invention may now be further understood by reference to thefollowing non-limiting illustrative examples.

FIG. 1 is a schematic process flow diagram illustrating one embodimentof the invention in which the fixed bed of porous particles is loaded ina dedicated stand alone vessel (V12) as part of a melt phase process forthe manufacture of the compositions of the invention. The zone V11represents an esterification zone in which a diacid and diol, forexample, terephthalic acid (TPA) and ethylene glycol (EG), areesterified in one or multiple vesses, such as continouous stirred tankreactors or a pipe reactor. The product of the esterification zone, suchas an oligomer mixture stream, is delivered to the purification vesselV12 via pipe C11 either through gravity or a pump at a LHSV ranging 1 to15. A heat exchanger may be included in the design of C11. If thetemperature within the V11 vessel is about same as the temperature inthe V12 vessel, a heat exchanger may not be needed. However, C11 shouldbe thermally insulated so that the esterification product will not besolidified in C11 in route from V11 to V12.

Hydrogen is introduced to V12 via C12 pipe by a compressor at a GHSVranging from 100 to 400. V12 is packed with the porous materials pelletssized from 0.5 mm to 3 mm and maintained at temperature within a rangeof 200° C. to 280° C. and pressure of 50 psig to 150 psig.

The hydrotreated PET oligomer is discharged from V12 and introduced to apolycondensation zone V13 via pipe C13 by either gravity or a pump. Theblock V13 represents a polycondensation process to polyester (PET) andthe final product is discharged via C15 through a pump or extruder. As astandard process practice, C13 may be equipped with thermal insulatingmaterials and heat exchanger if needed, and installed with variousvalves such as control valve to control the pressure of V12. Agas-liquid separator may be located between C13 and C14, and preferablybetween V12 and V13. The gas effluent from V12 may be recycled via C14and C12 back to V12 or not recycled, which may depend on the processeconomics or the purity requirements of the V12 hydrogen feed. Acondenser or separation column may be used to remove liquid moietiesfrom the recycled gas stream.

In comparison with FIG. 1 a, FIG. 1 b shows another configuration of theprocess in which the esterification products from V11 may be split intotwo streams; one oligomer stream is taken as a side draw and introducedto V12 for hydrotreating and the other stream introduced directly to V13for polycondensation. The split ratio may be determined according to thedesired properties of both the feed and the product required for theultimate application.

FIG. 2 is a schematic process flow diagram illustrating hydrotreating amolten polyester polymer stream. The zone V21 represents anesterification zone as described with respect to V11 in FIG. 1. Theoligomer mixture made in the esterification zone is fed to zone V22, aprepolymer zone, and then introduced via C21 to the zone V23 forhydrotreating. The operation condition surrounding V23 may be within thesame ranges described in FIG. 1 with respect to V12, but at a highertemperature and lower pressure to simulate the operating conditions ofthe prepolymer reaction zone V22 or the finishing zone V24. The treatedprepolymer undergoes further polycondensation or finishing in a one or anumber of finishing vessels or high polymerizer in zone V24 and thefinal product is discharged via C25. As FIG. 2 shows, the zone V23 andthe zone V24 may be operated in separate units (FIG. 2 a) or in anintegrated unit with the high polymerizer vessel split into differentzones within the same vessel. (FIG. 2 b). C24 is the hydrogen gasoff-take from a gas separator located between V23 and V24 as in FIG. 2a, or a gas discharge from the hydrotreating zone within the highpolymerizer.

FIG. 3 illustrates a process flow diagram in which the molten polyesterstream from a polycondensation zone (V32) is used as the feed to thefixed particle bed. The zone V31 represents a process of esterificationand oligomerization as described in FIG. 1. The zone V32 represents apoly-condensation process as described in FIG. 1. The molten polyesterstream having an It.V. of at least 0.55 from V32 is introduced to V33for hydrotreating via C31. C34 is the off-take of hydrogen gas from thehydrotreating zone V33 which is recycled directly or indirectly to C32hydrogen gas feed.

FIG. 4 illustrates a process flow diagram in which amorphous solidpolyester polymers or crystallized polyester polymers or solid statepolymerized polyester polymers, either in the form of virgin particles,scrap, or post consumer recycle polymer, is melted, or diluted with asolvent such as ethylene glycol, or de-polymerized, and fed to a vesselloaded with the porous particles to reduce the metal content of thepolymer stream. A PET is fed to the zone V41 in which it is melted, ordiluted with a solvent, or de-polymerized mechanically or chemically(such as methanolysis). Then, it is introduced via C41 to the zone V42for hydrotreating in a vessel in which hydrogen gas is fed via line C42and optionally recycled back directly or indirectly to the hydrotreatingvessel V42 via line C44 from the discharge line C43.

The following working examples demonstrate the removal of a variety ofmetal species from molten polyester polymers by flowing the moltenstreams over fixed beds of various non-catalytic porous materials.

COMPARATIVE EXAMPLE 1

78 g of carbon granules (¼″ in diameter) having a surface area of 1100m²/g, a median pore diameter of 3.1 nm, and pore volume of 0.3 cc/gcommercially available from Engelhard Corporation was loaded in a 1″ IDstainless steel reactor. Then the reactor was heated to 260° C. at aheating rate of 10° C./minute in flowing nitrogen at a rate of 60 GHSVand gradually pressurized to 150 psig. Then a PET pre-polymer wasprepared by the reaction of ethylene glycol and terephthalic acid in a1.3/1 mole ratio at 260° C. for 2 hours. The prepared oligomer had adegree of polymerization of 3.8, and contained 54.4 ppm cobalt. It wasfed to the reactor with an extruding pump at a LHSV of 1.8. Cobaltconcentration in the reactor effluent was determined with X-rayfluorescence spectroscopy and was found to be the same as theconcentration of the starting material. Without the presence ofhydrogen, cobalt could not be removed.

EXAMPLES 2-5

78 g of carbon, the same as used in Example 1, was loaded in a 1″ IDstainless steel reactor. To the reactor was added a flow of nitrogen gasat a rate of 60 GHSV at ambient temperature for 30 minutes. Then, thegas flow was switched from nitrogen to hydrogen gas, comprised of anexcess of 90 vol % hydrogen, at the same rate. Then, the reactor washeated to 260° C. at a heating rate of 10° C./minute in flowing hydrogengas. Then, the reactor was gradually pressurized to 50 psig withhydrogen. Then a PET pre-polymer containing 54.4 ppm cobalt was fed tothe reactor with an extruding pump at a LHSV of 1.8. Cobaltconcentration in the reactor effluent was decreased to 4.4 ppm from 54.5ppm in the starting material. The presence of hydrogen and carboneffectively removed cobalt from the molten polyester polymer stream. Coin Temperature/ Pressure/ the effluent/ Examples ° C. psig ppm 2 260 504.4 3 260 200 1.9 4 280 200 1.8 5 280 50 3.6

EXAMPLES 6-9

100 g of silicon carbide pellets (⅛″ in diameter) having a surface areaof 1 m²/g and average pore diameter of 5.5 nm (Engelhard Corporation)was loaded in a 1″ ID stainless steel reactor. Then the reactor washeated to 250° C. in flowing nitrogen and then hydrogen was added at arate of 60 GHSV from the same source as Example 2. Then, the reactor wasgradually pressurized to 100 psig. Then a PET pre-polymer containing54.4 ppm cobalt was fed to the reactor with an extruding pump at a LHSVof 1.8. Cobalt concentration in the reactor effluent was decreased to2.5 ppm from 54.5 ppm in the starting material. Co in Temperature/Pressure/ the effluent/ Examples ° C. psig ppm 6 250 100 2.5 7 260 1002.4 8 270 150 2.0 9 270 200 1.0

EXAMPLES 10-12

85 g of alumina having a surface area of 100 m²/g, pore volume of 0.5cc/g, and pore diameter 19.3 nm (Engelhard Corporation) was loaded in a1″ ID stainless steel reactor. Then the reactor was heated to 260° C. inflowing nitrogen and then hydrogen added at a rate of 60 GHSV from thesame source as Example 2. Then, the reactor was gradually pressurized to150 psig. Then a PET pre-polymer containing 54.4 ppm cobalt was fed tothe reactor with an extruding pump at a LHSV of 1.8. Cobaltconcentration in the reactor effluent was decreased to 13.4 ppm from54.5 ppm in the starting material. Co in Temperature/ Pressure/ theeffluent/ Examples ° C. psig ppm 10 260 150 13.4 11 260 90 13.6 12 26050 17.5

EXAMPLES 13-15

45 g of graphite pellets ( 1/16″ in diameter) having a surface area of620 m²/g, pore volume of 0.4 cc/g, and pore diameter of 3.2 nm(Engelhard Corporation) was loaded in a 1″ ID stainless steel reactor.Then the reactor was heated to 260° C. in flowing nitrogen and thenhydrogen at a rate of 60 GHSV from the same source as Example 2. Then,the reactor was gradually pressurized to 150 psig. Then a PETpre-polymer containing 54.4 ppm cobalt was fed to the reactor with anextruding pump at a LHSV of 1.8. Cobalt concentration in the reactoreffluent was decreased to 9.0 ppm from 54.5 ppm in the startingmaterial. Co in Temperature/ Pressure/ the effluent/ Examples ° C. psigppm 13 260 150 9.0 14 270 150 11.0 15 270 100 15.0

EXAMPLES 16

45 g of graphite, the same as described in Examples 13-15, was loaded ina 1″ ID stainless steel reactor. Then the reactor was heated to 260° C.in flowing nitrogen and then hydrogen added at a rate of 60 GHSV fromthe same source as Example 2. Then, the reactor was graduallypressurized to 150 psig. Then a PET pre-polymer containing 76 ppmantimony was fed to the reactor with an extruding pump at a LHSV of 1.8.Antimony concentration in the reactor effluent was decreased to 18 ppmfrom 76 ppm in the starting material.

1. A process for removing metal species from a composition comprisingcontacting: a. an oligomer mixture stream comprising the monomers of apartially aromatic polyester polymer and at least one metal species, orb. a molten polyester polymer stream comprising partially aromaticpolyester polymers and at least one metal species, with a non-catalyticporous material in the presence of a gas comprising, hydrogen to producea treated stream containing a reduced amount of at least one metalspecies.
 2. The process of claim 1, wherein the metal species comprisescobalt, antimony, titanium, manganese, zinc, calcium, or mixturesthereof.
 3. The process of claim 2, wherein the amount of at least oneof said metal species is reduced by at least 50%.
 4. The process ofclaim 3, wherein the amount of at least one of said metal species isreduced by at least 75%.
 5. The process of claim 1, wherein the moltenpolyester polymer stream comprises a partially aromatic polyesterpolymer having an It.V. of at least 0.2 dL/g.
 6. The process of claim 5,wherein the It.V. is at least 0.3 dL/g.
 7. The process of claim 1,wherein the porous material comprises carbon, graphite, activatedcarbon, silicon carbide, alumina, or silica.
 8. The process of claim 1,wherein the pore volume of said porous material ranges from 0.1 cc/g to0.8 cc/g, and the pore diameter ranges from 0.8 nm to 40 nm.
 9. Theprocess of claim 1, wherein the surface area of said materials rangefrom 0.5 to 2000 m²/g.
 10. The process of claim 1, wherein the LHSV ofthe molten polyester polymer stream over the fixed bed is a valueranging from 0.2 to 40, and GHSV of hydrogen over the fixed bed is avalue ranging from 5 to
 1000. 11. The process of claim 10, wherein themolten polyester polymer stream is contacted with hydrogen under apressure ranging from 10 to 2000 psig, and the temperature of the moltenstream ranges from 150 to 300° C.
 12. The process of claim 1, whereinthe metal species comprises cobalt reduced by at least 50% to an amountof less than 20 ppm.
 13. The process of claim 1, wherein at least aportion of at least one metal species is adsorbed onto the porousmaterial, the thereafter at least one of metal species adsorbed onto theporous material is recovered.
 14. The process of claim 1, comprisingesterifying reactants in an esterification zone in the presence of metalspecies to form an oligomer mixture comprisingbis-hydroxyalkylterephthalate monomers and metal species, followed bypolycondensing said oligomer mixture in a polycondensation zone,optionally in the presence of additional amounts of metal species and/ordifferent types of added metal species, to form a molten polyesterpolymer, and thereafter solidifying the molten polyester polymer,wherein after the oligomer mixture is formed and before the moltenpolyester polymer is solidified, at least a portion of the oligomermixture or molten polyester polymer contacts a fixed bed of thenon-catalytic porous material.
 15. The process of claim 1, comprisingforming a preform produced from a polyester polymer composition obtainedfrom said treated stream.
 16. The process of claim 1, comprising forminga beverage bottle produced form a polyester polymer composition obtainedfrom said treated stream.
 17. The process of claim 1, wherein theoligomer stream or molten polyester polymer stream flows over a fixedbed of said porous material.
 18. The process of claim 1, comprisingesterifying reactants in an esterification zone comprising two or moreesterification reactors, and contacting the oligomer mixture from thefirst esterification reactor with the porous material to produce atreated stream, and feeding the treated stream to a secondesterification reactor.
 19. The process of claim 18, wherein theoligomer mixture flow across a fixed bed of said porous material. 20.The process of any one of claims 1-19, wherein the gas comprises atleast 50 vol % hydrogen.
 21. The process according to any one of claim1-19, wherein the gas comprises at least 80 vol % hydrogen.
 22. Acomposition comprising partially aromatic polymers, containing repeatingunits of alkylene terephthalate or alkylene naphthalate, having an It.V.of at least 0.50 produced in a direct esterification melt phase process,from greater than 0 to less than 50 ppm antimony, and less than 40 ppmcobalt.
 23. The composition of claim 22, containing less than 10 ppmgermanium.
 24. The composition of claim 22, wherein composition containsless than 5 ppm titanium, less than 20 ppm zinc, less than 20 ppmmanganese, less than 20 ppm calcium, and less than 20 ppm magnesium. 25.The composition of claim 22, wherein the polymers are amorphous solidshaving an It.V.of greater than 0.72 dL/g obtained without solid statepolymerization.
 26. The composition of claim 22, wherein the compositionis a partially crystallized solid having a degree of crystallinity of atleast 25% and an It.V. of at least 0.70 dL/g obtained without solidstate polymerization.
 27. The composition of claim 26, wherein the It.V.of the polymers are least 0.70 dL/g obtained without solid statepolymerization.
 28. The composition of claim 22, wherein the compositionis a solid which contains less than 5 ppm titanium, less than 20 ppmzinc, less than 20 ppm manganese, less than 20 ppm calcium, less than 20ppm magnesium, and less than 10 ppm germanium.
 29. The composition ofclaim 28, wherein the polymer has an It.V. of greater than 0.72 dL/gobtained without solid state polymerization.
 30. A compositioncomprising partially aromatic polyester polymers, containing repeatingunits of alkylene terephthalate or alkylene naphthalate, having an It.V.of at least 0.50 dL/g produced in an ester exchange melt phase process,from greater than zero to less than 5 ppm titanium, and less than 10 ppmmanganese.
 31. The composition of claim 30, containing less than 10 ppmgermanium.
 32. The composition of claim 30, wherein composition containsless than 5 ppm titanium, less than 20 ppm zinc, less than 20 ppmmanganese, less than 20 ppm calcium, and less than 20 ppm magnesium. 33.The composition of claim 30, wherein the polymers are amorphous solidshaving an It.V.of greater than 0.72 dL/g obtained without solid statepolymerization.
 34. The composition of claim 30 wherein the compositionis a partially crystallized solid having a degree of crystallinity of atleast 25% and an It.V. of at least 0.70 dL/g obtained without solidstate polymerization.
 35. The composition of claim 34, wherein the It.V.of the polymers are least 0.70 dL/g obtained without solid statepolymerization.
 36. The composition of claim 30, wherein the compositionis a solid which contains less than 5 ppm titanium, less than 20 ppmzinc, less than 20 ppm manganese, less than 20 ppm calcium, less than 20ppm magnesium, and less than 10 ppm germanium.
 37. The composition ofclaim 36, wherein the polymer has an It.V. of greater than 0.72 dL/gobtained without solid state polymerization.